CN101778958A - The method of normal pressure acid leaching of laterite - Google Patents
The method of normal pressure acid leaching of laterite Download PDFInfo
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- CN101778958A CN101778958A CN200880102470A CN200880102470A CN101778958A CN 101778958 A CN101778958 A CN 101778958A CN 200880102470 A CN200880102470 A CN 200880102470A CN 200880102470 A CN200880102470 A CN 200880102470A CN 101778958 A CN101778958 A CN 101778958A
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- saprolite
- limonite
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/043—Sulfurated acids or salts thereof
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
- C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
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Abstract
Reclaim the normal pressure leaching method of nickel and cobalt from laterite ore, described method comprises the steps: a) to provide the limonite and the saprolitic ores component of laterite ore; B) respectively limonite and saprolitic ores component are made slurry to produce limonite slurry and saprolite ore pulp; C) from the saprolite ore pulp, separate the mineral of any limonite type to produce the saprolite feed slurry; D) the saprolite feed slurry is milled or wet-milling; E) in elementary lixiviate step, with vitriol oil lixiviate limonite slurry; F) after finishing elementary lixiviate step basically, by saprolite feed slurry and leached limonite slurry are merged this saprolite feed slurry is imported leaching process in the secondary lixiviate step, and discharge sulfuric acid with auxiliary this saprolite feed slurry of lixiviate, wherein this saprolite feed slurry does not conform to the mineral of any limonite type basically before being imported into leaching process.
Description
Invention field
The present invention relates to the normal pressure acid leaching of laterite ores to reclaim the method for nickel and cobalt product.
More specifically, the present invention relates to continuously and jointly the acid leaching of laterite ores component and discard iron-residues matter reclaiming nickel and cobalt.Method of the present invention is specially adapted to handle whole laterite ore body, be that limonite and saprolite component are all in the successive reaction, this method realizes by following step: at first use sulfuric acid normal atmosphere and high to the temperature of boiling point lixiviate limonite ore component, the component of lixiviate saprolitic ores continuously then, wherein before lixiviate, the mineral of whole limonite types from saprolite, have been removed basically.
This method is specially adapted to handle laterite ore body, and wherein limonite components has high Fe containedly, and the saprolite component has high pyrrhosiderite content.
Background of invention
Laterite (nickeliferous) ore body mainly contains three kinds of components: limonite components, the saprolite component on the bed rock and the ore in the transitional zone between limonite and the saprolite under the table soil.Pyrrhosiderite that nickel-containing mineral in the limonite is soft and particle diameter is little and/or rhombohedral iron ore.Nickel-containing mineral in the saprolite mainly is thick siliceous phase, for example serpentine, noumeite, chlorite, nontronite and montmorillonite.Ore in the transitional zone not only contains limonite but also contain saprolite.Under the help of geology data and mining program, may separate limonite and saprolite via the screening of using design by particle diameter.Yet, in practice of Mining, be difficult to fully separate limonite and saprolite component.Therefore, the intersection of limonite and saprolite is entrained in to a certain extent the raw ore coexistence with saprolite and limonite components.
PCT/AU03/00309 (people such as H.Liu, QNI Technology PTY LTD) has described the normal pressure acidleach and has put forward (AAL) method, and its processing is deposited on whole laterite ores of three mine belts.In described method, under the temperature of height to 105 ℃ (or the boiling point under the normal pressure), limonite slurry (or low contain Mg component) mixed with concentrated acid and use the concentrated acid lixiviate.The iron level of the limonite of testing in the embodiment of this application generally is 40% to 43%, and the sulfuric acid dosage that is expressed as the weight ratio of sulfuric acid and dried limonite ore is 1.32 to 1.43.This is shown in each of 11 embodiment.Under the balance acidity of the 0g/L to 10g/L that forms pyrrhosiderite, used saprolite (or height contains the Mg component) shows good lixiviate reactivity and neutralising capacity.This is because the fact that this saprolite is not polluted significantly by limonite.
The mineralogy of laterite ore component changes according to the zone in ore source.Table 1 among the PCT/AU03/00309 illustrates the feature from different local in the world various laterite ore body.Ore used among the embodiment of PCT/AU03/00309 is from Jia Gedao (GagIsland), Indonesia.Because the extensive feature of different laterite ore body must adjustment reclaim the method for nickel and cobalt so that rate of recovery maximization from ore body.
The applicant has been found that, because the high Fe content of laterite ore body, high pyrrhosiderite and/or rhombohedral iron ore content in high Fe content in the limonite components and the saprolite component specifically, nickel recovery in the normal pressure leach extraction method suffers damage, because the lixiviate of saprolite component is reactive and neutralising capacity is lower.This is considered to owing to higher pyrrhosiderite or rhombohedral iron ore content in the saprolite component.
Contingent some problem when the invention is intended to overcome or improving the laterite of under atmospheric pressure, handling high Fe content.
The patent document that provides as prior art that this paper quotes or other content should not be considered to admit when the priority date of arbitrary claim, and this document or content are known or the information that comprises of this document or content is the part of common practise.
Summary of the invention
The present invention relates to the normal pressure acid leaching of laterite ores to reclaim the method for nickel and cobalt product.Particularly, the present invention relates under the temperature of normal atmosphere and high boiling point to acid, continuously and jointly the limonite of normal pressure acid leaching of laterite ores and saprolite component are to reclaim nickel and cobalt.Laterite ore can also comprise other ore type, for example montmorillonite, nontronite and serpentine ore component, and will be understood that in the mode of in method as herein described, handling limonite and saprolite component and handle these ore type together.
The present invention is specially adapted to the method that high especially and this ore of the iron level of ore wherein comprises a certain amount of transition ore, wherein be difficult to separate limonite and saprolite component by the selectivity mining or the back gradation of digging up mine, perhaps the character in mineral deposit makes the separation of mining back be not easy.Method of the present invention also is applicable to handles the ore that wherein limonite and saprolite are derived from different mineral deposits.
Therefore, the present invention relates to reclaim the normal pressure leach extraction method of nickel and cobalt from laterite ore, described method comprises the steps:
A) provide the limonite and the saprolitic ores component of laterite ore;
B) respectively limonite and saprolitic ores component are made slurry to produce limonite slurry and saprolite ore pulp;
C) from the saprolite ore pulp, separate the mineral of any limonite type to produce the saprolite feed slurry;
D) the saprolite feed slurry is milled or wet-milling;
E) in elementary lixiviate step, with vitriol oil lixiviate limonite slurry;
F) after finishing elementary lixiviate step basically, by saprolite feed slurry and leached limonite slurry are merged this saprolite feed slurry is imported leaching process in the secondary lixiviate step, and discharge sulfuric acid to assist this saprolite feed slurry of lixiviate;
Wherein this saprolite feed slurry is substantially free of the mineral of any limonite type before being imported into leaching process.
Owing to handled whole ore bodies, limonite ore behind the gradation generally is made up of the small particle size nickel-containing mineral, for example pyrrhosiderite and/or rhombohedral iron ore, but also can comprise the siliceous component of some thick saprolite enrichments, for example serpentine, noumeite, chlorite, nontronite and montmorillonite.Similarly, the saprolite component not only contains the saprolite component, also contains the fine particulate matter of some limonite enrichments, and this particulate matter is rich in pyrrhosiderite and/or rhombohedral iron ore.In fact, this method is applicable to and handles the laterite ore that pyrrhosiderite polluted that saprolite component wherein may be exceeded 30wt%.Particularly, the applicant has been found that the nickel in this pyrrhosiderite can not be extracted fully when saprolitic ores has higher pyrrhosiderite content, because the acidity in the secondary lixiviate step is not strong to being enough to destroy the pyrrhosiderite structure.
In most of laterite samples, pyrrhosiderite is main nickel-containing mineral phase, yet some laterite ore body contains a spot of nickeliferous rhombohedral iron ore mineral really.
Therefore, in a preferred embodiment of the invention, before the saprolite ore pulp is added into secondary lixiviate step, by wet screening, swirling flow or gradation, from this saprolite ore pulp, remove the mineral of limonite type, for example the oxide material such as pyrrhosiderite and/or rhombohedral iron ore of the iron enrichment of small particle size.
Before elementary lixiviate step, can also pass through wet screening, swirling flow or gradation, from limonite slurry, remove the mineral of saprolite type, for example thick siliceous component serpentine, noumeite, chlorite, nontronite and montmorillonite.Yet have been found that the mineral of removing whole limonite types just before lixiviate from the saprolite ore pulp have basically caused the raising of the overall nickel and the cobalt rate of recovery.
Detailed Description Of The Invention
Method of the present invention comprises at first digs up mine by selectivity or mining back gradation, and laterite ore is separated into its limonite components and saprolite component.Perhaps, can provide limonite and saprolite component from different places.
The type that depends on ore, limonite and saprolite component all contain thin and thick component at least to a certain degree.This is normally owing to limonite during gradation after the mining separates with the incomplete of saprolite component.Thin component generally is made up of the ore composition of limonite type, for example pyrrhosiderite and/or rhombohedral iron ore.Nickel is entrained in pyrrhosiderite and/or the rhombohedral iron ore mineral structure.Thick component generally is made of for example thick siliceous serpentine, nontronite and montmorillonite mineral the mineral constituent of saprolite type.
In one embodiment, method of the present invention comprises laterite raw ore gradation is become its limonite and saprolite component.This realizes by the selectivity mining or the mining back gradation that comprise the selectivity screening usually.This method is specially adapted to ore body, wherein cannot or hardly in time limonite and saprolite fitly be separated, and/or usually, all contain a large amount of thin and thick components in limonite and the saprolite component.This method also is applicable to the laterite ore body with high Fe content, for example, wherein the saprolite component can contain pyrrhosiderite and/or the rhombohedral iron ore greater than about 30%, and limonite components can contain pyrrhosiderite and/or rhombohedral iron ore greater than 85%, or greater than 45% iron level.
Behind the gradation of mining back, limonite and saprolite component are made slurry respectively.The water that can use fresh water usually or be substantially free of sodium, basic metal or ammonium ion at least prepares slurry, but can prepare slurry with salt solution or seawater.Have been found that gained limonite and saprolite slurry all can have to a certain degree thin limonite enrichment and the component of thick saprolite enrichment.
In elementary lixiviate step, in the reactor of first reactor or first series, come lixiviate limonite feed slurry with the vitriol oil.Usually under the temperature of normal atmosphere and high boiling point to 105 ℃ or lixiviate reagent, carry out this step.
Before elementary lixiviate step, can carry out size separation to reclaim the mineral that may be present in the saprolite type in the slurry to limonite slurry.This helps to reduce the extraction that acid consumed and improved nickel.
Most preferably, the reaction temperature as far as possible of elementary lixiviate step ground is high under atmospheric pressure to realize quick lixiviate.Nickel-containing mineral in the limonite ore is pyrrhosiderite and/or rhombohedral iron ore, and nickel is distributed in pyrrhosiderite or the rhombohedral iron ore matrix.Therefore, the acidity of elementary lixiviate step should be enough to destroy pyrrhosiderite/rhombohedral iron ore matrix to discharge nickel.Preferably, vitriolic dosage be dissolving in the ore surpass 90% nickel, cobalt, iron, manganese approximately and surpass 80% aluminium and the stoichiometric quantity of magnesium 100% to 140%.Depend on the relative content of iron and magnesium and the metal fall of expection, acid is preferably 1: 30 to 1: 65 with the weight ratio of limonite ore in the initial lixiviate step.
In order to discharge contained cobalt in asbolane or other similar Mn (III or the IV) mineral, to inject the limonite feed slurry such as the reductive agent of sulfur dioxide gas, inclined to one side bisulfite lithium or lithium sulfite and be lower than 1000mV (SHE) preferably redox-potential is controlled to be, thereby the cobalt rate of recovery that improves, and preferably be higher than 800mV (SHE) and minimize with formation with ferrous ion.Most preferably, the redox-potential with elementary lixiviate step is controlled at about 835mV (SHE).Under about 835mV (SHE), cobalt is almost fully discharged from asbolane, and (the Fe that almost do not have ferric ion
3+) be reduced into ferrous ion (Fe
2+).
In case finish elementary lixiviate step basically, by saprolite feed slurry and leached limonite slurry merging are imported the saprolite feed slurry in the secondary lixiviate step.
Before secondary lixiviate step, should carry out size separation mutually to the saprolite ore pulp with the pyrrhosiderite of from thick saprolite silicate heads, removing thin iron enrichment and rhombohedral iron ore.If from the ore of saprolite type, do not remove the mineral of any limonite type, then the pyrrhosiderite of iron enrichment and rhombohedral iron ore mineral facies can be in secondary lixiviate step by lixiviate fully, thereby cause overall nickel to extract rate variance.The mineral that separate the limonite type from the ore of saprolite type are usually by realizing by the size separation such as the whole bag of tricks of wet screening, swirling flow or gradation.
Preferably, after the size separation step, carry out the saprolite ore pulp mill or wet-milling so that separation efficiency is maximized.Preferably, the ore pulp with the saprolite type is ground to granularity less than 300 microns.Have been found that and grind the kinetics that strengthens lixiviate really, and increase the release of nickel-containing mineral in lixiviant.Preferably, before secondary lixiviate step, by milling or thick saprolite component is ground in wet-milling.
Depend on the rheology of slurry and the expectation composition of lixiviate product solution, the solids concn that is respectively applied in primary and secondary leached limonite and the saprolite feed slurry all is preferably 20% to 40% solids content.Test shows that the solids concn in limonite and the saprolite slurry all most preferably is about 25% to 30%.
In theory, the amount of the saprolite that adds in secondary lixiviate step should be about as much as the summation of free acid residual in the elementary lixiviate step and the acid that discharges from the iron of pyrrhosiderite form precipitation.For example, remained the residual free acid of about 20g/L to 30g/L, and during goethite precipitation, discharged the sulfuric acid (Fe that is equivalent to 80g/L to 100g/L of 210g/L to 260g/L from elementary lixiviate step
3+).If the amount of the saprolite slurry that can obtain is bigger and disproportionate, then can in secondary lixiviate step, add other acid.
In secondary lixiviate step, preferably redox-potential is controlled to be 700mV to 900mV (SHE), most preferably from about 720mV to 800mV (SHE).Preferred redox-potential in the secondary lixiviate step is lower than the redox-potential of elementary lixiviate step slightly, because saprolite contains ferrous ion, and the release of ferrous ion has reduced the redox-potential in the secondary lixiviate step.Therefore, do not need reductive agent to control the redox-potential in this stage in this method usually.In the secondary lixiviate step demand of reductive agent is depended primarily on the content of saprolitic ores, if, for example, a large amount of cobalts is arranged in the asbolane, some oxygenants such as dichromate are perhaps arranged in the saprolite lixiviate, then may need some reductive agents.
Normally, the ferrous ion (Fe of 0.5g/L to 3.0g/L
2+) formation and these reaction conditionss under stable acid concentration represent finishing of reduction and lixiviate after the secondary lixiviate step.The weight loss of limonite ore is usually greater than 80%, and the extraction yield of nickel and cobalt is greater than 90%.
Secondary lixiviate step comprises the lixiviate of simultaneous saprolitic ores and iron precipitation, preferably contains ferric oxide, ferrihydrite or the ferric hydroxide precipitate of the form of less vitriol as pyrrhosiderite, jarosite or other.
Usually in reactor different or serial reaction device, carry out secondary lixiviate step with the reactor of elementary lixiviate step.After finishing elementary lixiviate step, saprolite feed slurry (its can by randomly preheating) and leached limonite slurry are added in the reactor of secondary lixiviate step.Under the highest possible temperature, react, be preferably up to the boiling point of lixiviate reagent under 105 ℃ or the normal atmosphere.Most preferably, this reaction temperature as far as possible ground is high to realize quick lixiviate and iron precipitation kinetics.
The invention still further relates to the recovery of nickel and cobalt after the leaching stages.Can be used for the recovery of nickel by many methods prepare still may to contain the ore iron level of a certain proportion of iron ion form after secondary lixiviate step extracting solution, described method comprises as described below these.
At first, can be by in the lixiviate slurry, adding such as Na
+, K
+, NH
4 +Jarosite form ion and jarosite seed crystal material, make the excessive iron ion stayed at the end of secondary leaching stages in the solution form precipitation with jarosite.Can add jarosite with the form of sodium sulfate, vitriolate of tartar or ammonium sulfate and form ion, perhaps jarosite formation ion may reside in the seawater or salt solution that once used during slurry preparation or the lixiviate processing.In this case, the other acid that discharges during precipitation as jarosite can be used in the other saprolitic ores of lixiviate.
Perhaps, can take to utilize the limestone slurry neutralization to force iron to be finished substantially so that the pyrrhosiderite form is sedimentary.As measuring at ambient temperature, the neutral terminal point is that pH is 1.5 to 3.0.
In other selection, shown in following reaction, can enough reductive agents excessive ferric ion be reduced into ferrous state such as sulfurous gas:
Fe
2(SO
4)
3+SO
2+2H
2O＝2FeSO
4+2H
2SO4????(1)
Reaction (1) also produces the other sulfuric acid that can be used in the other saprolite feed slurry of lixiviate.Can from the solution of gained, reclaim nickel and cobalt by for example using the sulfide precipitation in hydrogen sulfide or other sulfide source.Ferrous ion can not disturb this process, and can not pollute the sulfide precipitation thing.Perhaps, can use the extraction of blended precipitation of hydroxide, ion-exchange or liquid-liquid solvent that nickel and cobalt are separated with other impurity with ferrous ion in the extracting solution.It will be apparent for a person skilled in the art that the optional method that can adopt other finishes separating of iron and nickel and cobalt in the solution.
Preferably, make iron contain the ferric oxide of form of less vitriol or the form precipitation of ironic hydroxide as pyrrhosiderite or other, it contains seldom or sulfur-bearing hydrochlorate part not.This realizes by the water that uses fresh water or low at least sodium, basic metal and ammonium ion content usually.General reaction during the precipitation pyrrhosiderite is shown in the following reaction (2):
(Fe，Ni，)O.OH+(Mg，Ni)
3Si
2O
5(OH)
4+H
2SO
4FeO.OH+NiSO
4+MgSO
4+SiO
2+H
2O????(2)
Should general reaction be the combination of elementary limonite lixiviate step and secondary saprolite lixiviate step.
Similarly, iron is shown in the following reaction (3) with the general reaction of precipitated as jarosite:
(Fe，Ni)O.OH+(Mg，Ni)
3Si
2O
5(OH)
4+H
2SO
4NaFe
3(SO
4)
2(OH)
6+NiSO
4+MgSO
4+SiO
2+H
2O???(3)
When removing the iron of jarosite form from reaction mixture, every mole of sedimentary iron produces 1 mole acid.Yet when iron was precipitated with the pyrrhosiderite form, every mole of sedimentary iron produced 1.5 moles acid.Yet when using seawater or salt brine solution, regular meeting of Tie Tong is with the form precipitation of jarosite.
In secondary lixiviate step, most preferably making iron is the form precipitation of FeO (OH) with pyrrhosiderite, the higher levels of acid that can be used for secondary lixiviate step when this has obtained to make iron with precipitated as jarosite for example such as fruit.Being characterised in that especially owing to discharge sulfuric acid during the iron precipitation of secondary lixiviate step of the inventive method need do not added other sulfuric acid usually in this step.
The accompanying drawing summary
Fig. 1 illustrates the schema of the method for the invention.
Accompanying drawing describes in detail
Fig. 1 illustrates the schema of the preferred embodiment of the inventive method.The description that should be kept in mind that this schema is intended to describe the preferred embodiments of the invention, should not think that scope of the present invention is subjected to this description restriction.
Raw ore saprolitic ores (3) is pulverized (7).The saprolite (7) of raw ore limonite ore (1) and pulverizing is made slurry (9) for use fresh water, seawater or salt solution and starch to form limonite (13) and saprolite (15) (11).
Limonite and saprolite slurry not only comprise thin component but also comprise thick component separately.Thin component mainly is made up of limonite ore, and wherein nickel is contained in pyrrhosiderite and/or the rhombohedral iron ore.Thick component mainly is made up of saprolitic ores, and this saprolitic ores mainly is made up of the silicate minerals that comprises serpentine, noumeite, chlorite, nontronite and montmorillonite mineral.By wet screening, swirling flow or gradation, separate the thin limonite slurry of thick and thin component is substantially free of the saprolite type with generation mineral both and be substantially free of the thick saprolite slurry of the mineral of limonite type from limonite and saprolite slurry (being respectively 17 and 19).
In another embodiment,, saprolite slurry is carried out size separation,, then itself and limonite slurry are merged to isolate the mineral of limonite type by wet screening, swirling flow or gradation.Can limonite slurry self not carried out the size separation step to separate the mineral of saprolite type from limonite slurry.
To merge from the mineral of the thin limonite type of saprolite slurry and limonite slurry or the mineral that may once separate from the limonite type of limonite slurry, multiviscosisty (23), and underflow has formed limonite (elementary lixiviate) feed slurry (25).Overflow (26) can be recycled to slurrying step (9), separating step (17) or slurrying step (9) and separating step (17) both.
Thick saprolite component is merged, and wet-milling (27) and multiviscosisty (29), and underflow has formed saprolite (secondary lixiviate) feed slurry (31).Overflow (28) can be recycled to one or more slurrying steps (11), separating step (19) or wet-milling step (20).
In elementary lixiviate step (35), come lixiviate limonite feed slurry (25) with the vitriol oil (33) and sulfur dioxide gas (34).Sulfur dioxide gas is remained on 800mV (SHE) as reductive agent to the expected range of 1000mV (SHE) with the redox-potential with elementary lixiviate step.
When elementary lixiviate step when finishing or finishing, in secondary lixiviate step (37), saprolite feed slurry (31) and leached limonite slurry are merged.Can in this secondary leaching stages, add source such as the univalent cation of sodium sulfate, vitriolate of tartar and ammonium sulfate with auxiliary precipitation as jarosite (36).Generally make the form precipitation (39) of iron with pyrrhosiderite, jarosite or rhombohedral iron ore.
The extracting solution of gained is neutralized with Wingdale (41), thereby reclaim nickel and cobalt.Preferably but not necessarily, can be with this limestone slurry heating to improve the neutral reactivity.
Embodiment
Used in this embodiment and be derived from Indonesian laterite ore sample (" Indonesia " sample).The iron level of the limonite components of this Indonesia's sample is 49%.Mineralogical characteristic shows that the pyrrhosiderite content in limonite components and the saprolite component is respectively 92% and 35%.Find among the reactive and embodiment of neutralising capacity of the lixiviate of this saprolite sample used low from the laterite samples that adds the lattice island (" Jia Gedao " sample) than PCT/AU03/00309.
Indonesia's sample ore is carried out the normal pressure acidleach propose the compliance test.The result shows that the nickel recovery of the limonite components of Indonesia's sample meets expection, and the Ni rate of recovery of saprolite component is low.High pyrrhosiderite content (35%) in the saprolite component of Indonesia's sample has caused low reactivity, and this pyrrhosiderite is nonreactive in secondary lixiviate step.Therefore, the nickel that is embedded in the pyrrhosiderite can not be extracted fully.After 3 hours the limonite lixiviate, from limonite components, extracted about 98.7% nickel.Yet, after 11 hours the saprolite lixiviate, only from the saprolite component, reclaimed 54.2% nickel.Total extraction yield of nickel is 68%.
Table 1: the average chemical constitution (%wt) that adds lattice island and Indonesia's laterite samples
Table 2: the mineralogical composition that adds lattice island and Indonesia's laterite samples
*(%wt)
*: use XRD determining
*: comprise serpentine, enstatite and forsterite
Handle the improved normal pressure acidleach of laterite ore sample and put forward (AAL) method
The sour dosage and the solids concn of the control of starting raw material
Because the high Fe content in the limonite components of Indonesia's sample, find sulfiting agent quantity not sufficient used among the embodiment of PCT/AU03/00309 with the lattice that destroys pyrrhosiderite to discharge the nickel of embedding.With the sour dosage of limonite lixiviate, promptly the weight ratio of acid/limonite increases to 1.60 from 1.35-1.40.Table 3 illustrates the improvement of the nickel extraction yield of total nickel extraction yield and limonite and saprolite component.
Table 3: the nickel extraction yield that uses various sour dosage
| Test I D | Acid/limonite t/t | Total Ni extraction yield % | Limonite extraction yield % | Saprolite extraction yield % |
| ??1-1 | ??1.30 | ??56.0 | ??90.0 | ??38.0 |
| ??1-2 | ??1.44 | ??58.0 | ??91.0 | ??41.0 |
| ??2-1 | ??1.55 | ??67.5 | ??98.0 | ??52.3 |
| ??2-2 | ??1.60 | ??68.5 | ??98.7 | ??54.5 |
Attention: in test 1-1 and 1-2, used 30% limonite and saprolite slurry
In test 2-1 and 2-2, used 24% limonite and saprolite slurry
Although increase nickel and cobalt concentration that the solids concn of starting raw material can reduce the size of reactor and increase PLS, excessive spissated feed slurry also can cause the saturated of iron ion in the extracting solution.In case the Fe concentration in the solution reaches its saturated level, this solution can not dissolve more pyrrhosiderite.The normal pressure acidleach of Indonesia's sample ore is put forward the result and is shown, after 3 hours the limonite lixiviate, oversaturated Fe is～150g/L (when the solids concn of the slurry of importing is 30%).Table 3 shows, the solids concn of starting raw material is reduced to 24% from 30% promoted the ore leaching process, thereby improved the nickel extraction yield.
Embodiment 2:
The preparation of ore of carrying out Indonesia's laterite ore by wet screening is to handle limonite and saprolite component respectively.Screen size is 355 microns.Undersized component is merged into the limonite ore of supplying with AAL, not undersized component is merged into the saprolitic ores of supplying with AAL.Table 4 is illustrated under 355 microns the separation size, based on the result of the upgrading of the limonite of nickel, iron, magnesium and silicone content and saprolitic ores.
Table 4: the limonite of upgrading and saprolite are formed (%)
Wet screening hole size: 355 microns
Embodiment 3:
By size separation, Indonesia's laterite ore is carried out preparation of ore differently to handle the saprolite component.Table 5 to table 7 is illustrated in respectively under the separation size of 100 microns, 63 microns and 45 microns, based on the updating result of the gained saprolitic ores of nickel, iron, magnesium and silicone content.
Table 5: the saprolite of upgrading is formed (%)
Separation size: 100 microns
Table 6: the saprolite of upgrading is formed (%)
Separation size: 63 microns
Table 7: the saprolite of upgrading is formed (%)
Separation size: 45 microns
Embodiment 4:
Philippines's laterite ore is carried out preparation of ore to handle limonite and saprolite component.The average composition of the limonite components after the processing is 1.17% Ni, 42.3% Fe, 1.26% Mg, 5.5% Al and 3.47% Si.Under 45 microns separation size, handle the saprolite component by wet screening.Table 8 illustrates based on nickel, iron, magnesium and silicone content, the result of the upgrading that obtains on saprolite (surpassing size) component.
Table 8: the saprolite of upgrading is formed (%)
Separation size: 45 microns
Philippines's laterite ore is carried out the normal pressure acidleach propose compliance test, this ore is made slurry and multiviscosisty to obtain 25% to 28%w/w solids content in tap water (drinkable).Result shown in the table 8 shows that the nickel recovery from limonite components meets expection, and it is not high not carry out the nickel extraction yield of saprolite component of size separation.High pyrrhosiderite content in the saprolite component has caused low reactivity, and this pyrrhosiderite is nonreactive in secondary lixiviate step.Carry out size separation with after removing thin (45 microns) limonite components, nickel extraction yield and total nickel extraction yield of saprolite (surpassing size) all obviously improve.After table 9 shows and removes the thin component of limonite, the reduction of the concentration of iron of the end product solution that obtains by lixiviate.
Table 9: the nickel extraction yield of in tap water, making Philippines's laterite ore of slurry
| Test I D | Saprolitic ores | Acid/limonite t/t | Total Ni extraction yield % | Limonite Ni extraction yield % | Saprolite Ni extraction yield % |
| ??3-1 | In bulk | ??1.46 | ??73.4 | ??94.9 | ??54.1 |
| ??3-2 | Surpass size | ??1.38 | ??84.1 | ??97.1 | ??64.6 |
Table 10: the average composition (g/L) of the product solution that obtains from the normal pressure lixiviate of Philippines's laterite ore
| Test I D | Saprolitic ores | Acid/limonite t/t | Fe (all) g/L | ??F 3+g/L | ??pH |
| ??3-1 | In bulk | ??1.46 | ??39 | ??34 | ??1.2 |
| ??3-2 | Surpass size | ??1.38 | ??24 | ??20 | ??1.5 |
Description of the invention as herein described is intended to describe sign feature of the present invention.The modification that does not depart from the spirit or scope of the present invention as herein described that these features are made also is included in the scope of the present invention.
Claims (21)
1. reclaim the normal pressure leach extraction method of nickel and cobalt from laterite ore, described method comprises the steps:
A) provide the limonite and the saprolitic ores component of laterite ore;
B) respectively described limonite and saprolitic ores component are made slurry to produce limonite slurry and saprolite ore pulp;
C) from described saprolite ore pulp, separate the mineral of any limonite type to produce the saprolite feed slurry;
D) described saprolite feed slurry is milled or wet-milling;
E) in elementary lixiviate step, with the described limonite slurry of vitriol oil lixiviate;
F) after finishing described elementary lixiviate step basically, by described saprolite feed slurry and leached limonite slurry are merged described saprolite feed slurry is imported leaching process in the secondary lixiviate step, and discharge sulfuric acid with the auxiliary described saprolite feed slurry of lixiviate
Wherein said saprolite feed slurry is substantially free of the mineral of any limonite type before being imported into described leaching process.
2. the method for claim 1 wherein separates the mineral of described limonite type from described saprolite ore pulp by wet screening, swirling flow or gradation.
3. the method for claim 1 wherein before described elementary lixiviate step, is separated the mineral of any thick saprolite type from described limonite slurry.
4. method as claimed in claim 3 wherein by wet screening, swirling flow or gradation, is separated the mineral of described saprolite type from described limonite slurry.
5. the method for claim 1 wherein is ground to particle diameter less than 300 microns with the described saprolite component in the described saprolite feed slurry.
6. the method for claim 1, wherein in described secondary lixiviate step, add described saprolite feed slurry after, make iron contain ferric oxide, ferrihydrite or the ferric hydroxide precipitate of the form of less vitriol as pyrrhosiderite, ferrihydrite, jarosite or other.
7. the method for claim 1, the mineral of wherein said limonite type mainly are made up of oxide material, pyrrhosiderite and/or the rhombohedral iron ore of nickeliferous iron enrichment.
8. the method for claim 1, the solids concn in wherein said limonite and the saprolite feed slurry approximately is the 20%-40% solids content.
9. the method for claim 1, the mineral of wherein said saprolite type mainly are made up of thick siliceous component serpentine, noumeite, chlorite, nontronite and montmorillonite.
10. the method for claim 1, the acid in the wherein said elementary lixiviate step and the weight ratio of limonite are 1: 30 to 1: 65.
11. the method for claim 1 wherein under the temperature of normal atmosphere and high boiling point to 105 ℃ or lixiviate reagent, is carried out described elementary lixiviate step in the reactor of first reactor or first series.
12. the method for claim 1, wherein the sulfuric acid that in described elementary lixiviate step, adds be dissolving in the described ore surpass 90% nickel, cobalt, iron, manganese approximately and surpass 80% aluminium and stoichiometric quantity that magnesium is required 100% to 140%.
13. the method for claim 1 wherein under the temperature of normal atmosphere and high boiling point to 105 ℃ or lixiviate reagent, is carried out described secondary lixiviate step in one or more reactors different with the reactor of described elementary lixiviate step.
14. the method for claim 1 wherein after adding described saprolite feed slurry, is added sulfuric acid to replenish the sulfuric acid that discharges in described secondary lixiviate.
15. the method for claim 1 wherein is controlled to be the redox-potential in the described elementary lixiviate step and is lower than 1000mV (SHE) and reclaims to improve cobalt.
16. the method for claim 1 wherein is controlled to be the redox-potential in the described elementary lixiviate step and is higher than 800mV (SHE) and minimizes with the formation with ferrous ion.
17. the method for claim 1 wherein remains on 700mV to 900mV (SHE) with the redox-potential in the described secondary lixiviate step.
18., wherein control described redox-potential by in described slurry, injecting sulfur dioxide gas, inclined to one side bisulfite lithium or lithium sulfite as claim 15,16 or 17 described methods.
19. the method for claim 1, wherein in described secondary lixiviate step, add univalent cation so that iron with the form precipitation of jarosite.
20. method as claimed in claim 19, wherein said univalent cation is selected from sodium, potassium or ammonium.
21. the method for claim 1, it basically with reference to accompanying drawing or arbitrary embodiment as mentioned before.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2007904228A AU2007904228A0 (en) | 2007-08-07 | Atmospheric Acid Leach Process for Laterites | |
| AU2007904228 | 2007-08-07 | ||
| PCT/AU2008/001144 WO2009018619A1 (en) | 2007-08-07 | 2008-08-07 | Atmospheric acid leach process for laterites |
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| CN101778958A true CN101778958A (en) | 2010-07-14 |
| CN101778958B CN101778958B (en) | 2012-02-29 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2008801024701A Expired - Fee Related CN101778958B (en) | 2007-08-07 | 2008-08-07 | Atmospheric acid leach process for laterites |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US8366801B2 (en) |
| CN (1) | CN101778958B (en) |
| AU (1) | AU2008286193B2 (en) |
| CO (1) | CO6260157A2 (en) |
| WO (1) | WO2009018619A1 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102061381A (en) * | 2011-01-06 | 2011-05-18 | 广西银亿科技矿冶有限公司 | Method for bath leaching and extracting nickel and cobalt from garnierite |
| CN102534206A (en) * | 2012-02-23 | 2012-07-04 | 北京矿冶研究总院 | Leaching method of limonite type laterite-nickel ore |
| CN104611558A (en) * | 2014-12-31 | 2015-05-13 | 金川集团股份有限公司 | Method for recovering nickel, cobalt, iron and silicon from laterite-nickel ore through united leaching technology |
| WO2024178571A1 (en) * | 2023-02-28 | 2024-09-06 | 中国科学院过程工程研究所 | Two-stage normal-pressure hydrochloric acid combined leaching method for nickeliferous laterite ores |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US8802042B2 (en) | 2002-07-19 | 2014-08-12 | Vale S.A. | Process of recovery of base metals from oxide ores |
| EP2370607A1 (en) * | 2008-11-28 | 2011-10-05 | BHP Billiton SSM Development Pty Ltd | Process for separating limonite and saprolite |
| CN102301017A (en) * | 2009-02-02 | 2011-12-28 | Bhp比利通Ssm开发有限公司 | Method of agglomeration |
| US8954257B2 (en) * | 2012-09-13 | 2015-02-10 | GM Global Technology Operations LLC | Coordinated torque control security systems and methods |
| CN104120259B (en) * | 2014-07-30 | 2016-03-02 | 广西师范大学 | A kind of nickel oxide ore pickling liquor two step method for removing iron |
| AU2015252121B2 (en) | 2014-11-05 | 2020-10-22 | Scandium International Mining Corporation | Systems and methodologies for direct acid leaching of scandium-bearing ores |
| US9982326B2 (en) | 2014-12-22 | 2018-05-29 | Scandium International Mining Corp. | Solvent extraction of scandium from leach solutions |
| CN104611555B (en) * | 2014-12-31 | 2017-05-03 | 金川集团股份有限公司 | Method for extracting nickel, cobalt, iron, silicon and magnesium from limonite |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6261527B1 (en) * | 1999-11-03 | 2001-07-17 | Bhp Minerals International Inc. | Atmospheric leach process for the recovery of nickel and cobalt from limonite and saprolite ores |
| AUPS201902A0 (en) * | 2002-04-29 | 2002-06-06 | Qni Technology Pty Ltd | Modified atmospheric leach process for laterite ores |
| EP1841891A4 (en) | 2004-12-30 | 2008-06-25 | Bhp Billiton Ssm Tech Pty Ltd | Extraction of nickel and cobalt from a resin eluate stream |
| ES2394915T3 (en) * | 2005-02-14 | 2013-02-06 | Bhp Billiton Ssm Development Pty Ltd | Procedure for improved acid leaching of laterite minerals |
-
2008
- 2008-08-07 AU AU2008286193A patent/AU2008286193B2/en not_active Ceased
- 2008-08-07 US US12/672,351 patent/US8366801B2/en not_active Expired - Fee Related
- 2008-08-07 WO PCT/AU2008/001144 patent/WO2009018619A1/en active Application Filing
- 2008-08-07 CN CN2008801024701A patent/CN101778958B/en not_active Expired - Fee Related
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102061381A (en) * | 2011-01-06 | 2011-05-18 | 广西银亿科技矿冶有限公司 | Method for bath leaching and extracting nickel and cobalt from garnierite |
| CN102534206A (en) * | 2012-02-23 | 2012-07-04 | 北京矿冶研究总院 | Leaching method of limonite type laterite-nickel ore |
| CN104611558A (en) * | 2014-12-31 | 2015-05-13 | 金川集团股份有限公司 | Method for recovering nickel, cobalt, iron and silicon from laterite-nickel ore through united leaching technology |
| WO2024178571A1 (en) * | 2023-02-28 | 2024-09-06 | 中国科学院过程工程研究所 | Two-stage normal-pressure hydrochloric acid combined leaching method for nickeliferous laterite ores |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2008286193B2 (en) | 2011-10-27 |
| CO6260157A2 (en) | 2011-03-22 |
| US20110100163A1 (en) | 2011-05-05 |
| AU2008286193A1 (en) | 2009-02-12 |
| US8366801B2 (en) | 2013-02-05 |
| CN101778958B (en) | 2012-02-29 |
| WO2009018619A1 (en) | 2009-02-12 |
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